Carbon Block/Filtration Bed/Conical Reactor with Fluidized Bed System Allowing Small Sorbent Particles to Regenerate Fluid During Extracorporeal Blood Treatment

ABSTRACT

Methods and devices for powdered sorbent regeneration of biologic fluids are disclosed. The present invention includes three novel methods, which may be used singly or in any combination, for constraining or immobilizing powders so that they can be perfused with a biological fluid or dialysate: a porous carbon block filter, a filtration bed of very fine powder, and a cone-shaped reactor.

CROSS REFERENCE

This application is a divisional application of U.S. non-provisionalapplication Ser. No. 15/624,703/, filed Jun. 15, 2017, which claimed thebenefit of U.S. provisional patent application Ser. No. 62/350,189,filed Jun. 15, 2016, the disclosure of which is expressly incorporatedby reference.

FIELD

Methods and devices for powdered sorbent regeneration of biologicfluids.

BACKGROUND

Toxins in the body (human or animal) may be of either external origin ora result of physiologic processes. Where renal or hepatic failure orinsufficiency hampers normal metabolism or excretion of waste productsor toxins, serious illness or death results, even though the wasteproducts or toxins may be normally present in the body in non-toxicconcentrations.

Although antidotes sometimes may be employed for specific toxins, at thepresent time, treatments for toxins in the body typically involve eitherreplacement of body fluids (e.g., blood or plasmareplacement/transfusion) or purification of the blood by external means.An example of such blood purification is the fairly common process ofrenal dialysis (either standard or peritoneal). In the most commonmethods of dialysis, highly pure water on one side of a membrane (e.g.,the peritoneum or an artificial membrane in a dialyzer) is used tocreate osmotic transport of toxins from the blood to the water. Thewater, after passing once through the dialyzer, is discharged to thedrain. In a standard dialysis system, the patient's blood is pumpedthrough the dialyzer, while the highly pure water, combined withessential electrolytes, is passed through the dialyzer on the oppositeside of the dialyzer membrane.

Where a large supply of highly pure water is not available orundesirable, it is possible to re-circulate the dialysis water bypurifying it. Such purification is accomplished with active carbon,often in conjunction with ion-exchange media. The Redy™ 2000 andAllient™ dialysis machines are examples of such a system. In thesemachines, the dialysate is purified (regenerated) by layers of granularcarbon and ion exchange resins in a single cartridge (the Sorb™ column).In principle, multiple cartridges, each containing a single substance,could be connected in series to achieve the same result. The activecarbon adsorbs various toxins. Hemodialysis circuits are typicallyclean, but not sterile. The Sorb column is also clean, but not sterileand the carbon layer actually removed many bacteria. Since the dialysistreatments of the Redy and Allient machines were of limited duration, upto 8 hours, recirculating dialysate through the Sorb column did notresult in significant growth of bacteria in the dialysate.

Another method of blood purification is hemoperfusion, where thepatient's blood is pumped directly through a bed of granular activecarbon. The active carbon adsorbs toxins directly from the blood. Thismethod is rarely used due to thrombogenicity and other issues.

In other, typically more recent and experimental extracorporealtreatments, plasma is separated from the patient's blood by a filter orcentrifuge. The plasma is then treated by contact with purificationmedia such as active carbon and/or ion exchange media, which adsorbtoxins from the plasma.

Of interest here is the role of active carbon. Carbon is a naturaladsorbent for many organic compounds including toxins. Thermal, steam,or chemical treatment of carbon can create a highly porous form ofcarbon with very high surface area per unit weight, typically on theorder of 100 to 2000 square meters per gram. Such treated carbon iscalled, variously, activated carbon, activated charcoal, active carbon,active charcoal, etc. The term “active carbon” is used herein. The porestructure of active carbon is commonly classified according to size asmacropores, mesopores and micropores. See FIG. 1. It is the porestructure which gives active carbon its high surface area per unitweight, and thus its “activity” or affinity which enables it to adsorbsignificant and useful quantities of toxins. Toxins thus adsorbed arethus, obviously, removed from the patient.

Pores typically become finer as one penetrates deeper into a particle ofcarbon. The larger, outer, macropores lead to the smaller mesopores(variously defined as being 2-100 μm), which in turn, lead to the yetsmaller micropores (variously defined as <2-10 μm).

Since adsorption is a physical, equilibrium-governed process, particlesof carbon will rapidly and immediately adsorb a small initial charge oftoxin, but then adsorption will cease unless the toxin diffuses into thepore structure of the carbon particle where the toxin is able to reachareas of low toxin concentration. Hence, diffusion of the toxin into theinterior pore structure is critical as most of the available surfacearea of the carbon is in the pore structure, particularly the mesoporesand micropores. This being the case, highly microporous carbons aretypically selected for small molecular weight toxins and highlymesoporous carbons are typically selected for larger molecular weighttoxins. Where mixes of toxins are encountered, a carbon with a mix ofmesopores and micropores will be selected.

Many processes govern diffusion of molecules into the pores. Ingeneralhowever, the longer the pore, the more time it will take fortarget molecules to reach the inner portions of the pores. The result isthat the larger the particle of active carbon, the slower the diffusionof target (toxin) molecules into the pores and the slower the adsorptionkinetics, other parameters being equal.

One obvious method of reducing the mean path length of the porestructure is to use smaller particles of carbon. Whereas industrialpurification processes typically use granular carbon and treatment timesof hours, carbon given as general oral antidote for poisoning is finelypowdered.

FIG. 2 compares the effects of particle size on adsorption kinetics. InFIG. 2, reaction time was limited. During this time, the same granuleswhich adsorbed little bilirubin (a typical toxin) adsorbed much morebilirubin when powdered. The very finely powdered oral adsorbent used asa general antidote to accidental poisoning (Norit Powder) adsorbed verymuch more bilirubin.

This phenomenon, at its core, is simple: Smaller particles have shortermean pore length so they adsorb toxins more quickly.

When active carbon is used as an oral sorbent, or when employed in asuspension, very fine particles rapidly adsorb toxins and are thus muchmore effective than larger particles where time of contact between theactive carbon and the solution containing the toxins is limited.

FIG. 3 is presented as an example of a use of fine particles of activecarbon as an adsorbent to detoxify patient blood. The diagram shows anextracorporeal system using a suspension of finely pulverized (<10 μm,typical) active carbon. Blood is pumped from the patient through afilter, which may be a plasma filter, dialyzer or similar device. Thefiltrate (e.g., dialysate, albumin, or patient plasma) is passed througha reactor which mixes fine active carbon particles with the treatedfluid, separates the treated fluid from the carbon, and returns thetreated fluid either to the dialyzer or directly to the patient. Thistype of system is relatively fast and is therapeutically effective, butis costly and complex due to the need to separate very fine carbonparticles from the exiting fluid.

It is important to note that in most cases, fluid volume is a criticallimitation. There are two such limitations. First, to provide adequatetreatment, i.e., to remove a clinically significant amount of toxin fromthe patient, a large volume of the patient's blood must be treated in areasonable amount of time. Since treated blood is returned to thepatient immediately, toxin removal follows an exponential decay curve.Secondary processes include diffusion of toxins from the interstitialfluid to the blood and from cells to the interstitial fluid and blood.FIG. 4 shows theoretical toxin removal by a perfect adsorbent over timefor various plasma flow rates for a particular system which used aplasmafilter and an active carbon sorbent to treat rat plasma in amanner similar to that of FIG. 3, but which used solid block carbon.

As may be seen, improvements in plasma flow rate (Q) produceimprovements in toxin clearance. The reason for this is that over agiven period of time, higher flow rates treat more of the patient'sblood and thus remove more toxin.

While the first volume limitation mandates a high treated fluid volume,safety considerations dictate that only a limited amount of blood may bewithdrawn from a patient at any one time. Extracorporeal systemsnecessarily withdraw blood from the patient and present not only ashort-term loss to the patient, but also present a hazard of long-termblood loss in the event of machine failure or clotting in the system.Hence, there is a second fluid volume limitation in that only a minimalamount blood is available for treatment at any one time.

In a particular practical extracorporeal system treating plasma, forexample, plasma is presented to the active carbon for only sevenminutes. Rapid adsorption kinetics is thus a necessity. Even in the caseof regenerating aqueous dialysate, there may be practical fluid volumelimitations, particularly when it is necessary to retain patientnutrients and desirable blood components which would otherwise be lostin standard “down the drain” hemodialysis.

As noted above, small particles may be used in a stirred suspension, butthe apparatus is complex and costly. Packed columns would, at first,appear to be a reasonable alternative. Unfortunately, small particlespresent substantial hydraulic resistance when packed into a column.Making a column shorter and of increased cross-sectional area producesbenefits, but this method has severe limitations due to problems withchanneling in the charcoal bed, lack of even flow distribution andmechanical constraints. The problem is greatly compounded when theactive carbon must treat proteinaceous fluids such as albumin or plasmawhich are viscous. The matter is more severe yet when column outletfrits (filters) must pass very large molecular weight substances foundin plasma such as albumin and globulins. Carbon particle fines in theoutlet frit may reduce the effective frit pore size to such smalldimensions as to produce molecular sieving, a phenomenon which theinventors have observed. In certain cases, using high pressure canovercome some of these limitations, but this is costly, particularlywhere biohazard considerations dictate disposable wetted pumpcomponents.

We are thus left with the quandary that small particles givetherapeutically useful fast sorption kinetics, while large particles maybe readily contained in inexpensive columns which treat fluid atreasonable pressures. It is the object of the present invention toresolve this conundrum.

In general principle, an approach to providing a short mean diffusionpath length in the pore structure of the carbon, while using large,easily-constrained carbon pieces, is to use large carbon pieces whichare “geometrically complex” and which have a fine structure. A spongeroughly illustrates the concept. The sponge is a large object, but ithas relatively small features. If the geometrically complex carbon isporous and allows the treated fluid to pass through it, then the usefulfast reaction kinetics of small particles is provided by the smallfeatures. The overall particle is large and easily constrained in areactor.

It is important to clarify some terminology at this point. Active carbonhas a large surface area which is created by the pore structure. But wemay define, “gross surface area,” as that surface which is presented bythe outer surface outside of the pore structure. For example, generallyspherical carbon particles of any size would have gross surface area of4πr². Obviously, the distinction between “gross surface” and thebeginnings of the pores is fuzzy, but this does not invalidate theusefulness of the concept.

We desire pieces of carbon which have high gross surface area and finefeatures which give a short mean pore path length.

One form of geometrically complex active carbon that has been developedis fractal spherical carbon developed by Vladimir Nikolaev as shown inFIG. 5 which is used for hemoperfusion.

This carbon has performed well in specific applications, but is costly,not readily available and the spheres must be confined in a column by afrits or other means. Since the particles are on the order of 100 μm,pressure drop through a column, while not excessive, is significant,especially for plasma treatments.

SUMMARY

Extracorporeal blood treatments remove blood from a patient, purify itin some manner and return the blood to the patient. Standardhemodialysis is an example of such treatments. Some extracorporeal bloodtreatments use active carbon sorbents to adsorb various toxins from theblood (directly or indirectly) and it is this type of treatment to whichthe present invention applies. While in hemoperfusion, the carboncontacts the blood directly, more typically, patient plasma or anothercirculating fluid contacts the active carbon.

In order for an extracorporeal blood treatment to be effective inremoving toxins from a patient's body, a substantial volume of fluidmust be treated. At the same time, safety and physiological constraintslimit the amount of blood that can be removed from the patient at anyone time. Other constraints also typically limit the amount of fluidavailable for sorption treatment at any one time. The naturalconsequence of these two simultaneous limitations is that a treatmentdevice has only a few minutes in which to adsorb the toxins from thetreated fluid. As a result, sorption kinetics must be sufficiently rapidor the device will be ineffective.

It is in the nature of active carbon sorbents that fluid containingtoxins to be adsorbed (and thus removed from the patient) must diffuseinto the pore structure of the carbon, a process which takes a certainamount of time. Given a certain otherwise same set of diffusionconditions, and especially for larger molecular weight toxins, it isobvious that the shorter the mean path length of the pore structure, themore rapidly the active sites in the carbon will be utilized and thusthe more rapidly the toxin will be adsorbed. It is for this reason thatcommonly used large granules of active carbon have sorption kineticswhich are too slow for effective and efficient extracorporeal use,especially for toxins of more than a few hundred Daltons molecularweight.

One obvious way to achieve a short mean pore path length is to use smallparticles of carbon as opposed to the larger granules in common use.However, active carbon in the form of small particles is difficult touse. If used in a stirred suspension, separation of the treated fluidfrom the suspension after treatment is difficult. If the small particlesare packed into a column, pressures are excessive, particularly withproteinaceous fluids. The common opinion of chemical engineers is thatit is impossible to construct a column with even flow distribution andmodest pressure drop from particles smaller than 50 microns, and eventhat particle size works in a column only if the particles are nearlyperfectly spherical.

In general principle, an approach to providing a short mean diffusionpath length in the pore structure of the carbon, while using large,easily-constrained carbon pieces, is to use large carbon pieces whichare “geometrically complex” and which have a fine structure. A spongeroughly illustrates the concept. The sponge is a large object, but ithas relatively small features. If the geometrically complex carbon isporous and allows the treated fluid to pass through it, then the usefulfast reaction kinetics of small particles is provided by the smallfeatures. The overall particle is large and easily constrained in areactor. We desire very small pieces of carbon which have high externalsurface area and fine features which give a short mean pore path length,but which are constrained or immobilized in a manner to allow perfusionof fluids around every particle. Commonly available commercial drinkingwater filters made of porous powdered carbon extruded with fine plasticfibers have this desirable complex geometry, being constructed ofpowders ranging from 1 to 20 microns in size and having short mean porepath length. The fluid pathways in such carbon blocks may range from afraction of a micron to five microns, and thus the surface acts as avery uniform filter preventing passage of larger particles. Thus, thecarbon block would not be suitable for blood perfusion, but would besuitable for treating other biological fluids such as plasma orperitoneal fluid or dialysate which is a salt solution which accumulatestoxins from blood by passage across semipermeable membranes. Thefiltering surface of the carbon block is also of benefit for restrainingvery small particles of other sorbents besides charcoal.

The present invention includes three novel methods, which may be usedsingly or in any combination, for constraining or immobilizing powdersso that they can be perfused with a biological fluid or dialysate:

A porous carbon block (CB) filter (such as is typically used as drinkingwater filters) is used to regenerate fluid during extracorporeal bloodtreatments. Surprisingly, we know of no medical device that currentlyincludes a carbon block for removing toxins, either from any dialysateor any biological fluid.

A filtration bed (FB) of very fine powder which is created by passing afluid containing suspended particles through the filtering surface ofthe carbon block (or a similar filter) and then holding the particles infixed position by continued fluid flow. This filtration bed allowsparticles of a few microns diameter to be used for perfusion anddepuration like a column, but breaking the above described “50 micron”rule and providing even flow distribution within the layer of very smallparticles.

A cone-shaped reactor (CR) designed to suspend particles in a “fluidizedbed” in which an upward flow of dialysate or biological fluid exactlyequals the sedimentation rate of fine particles. The particles then movearound within the suspension of fluid, mixing evenly with all thepassing fluid. The conical shape provides a continuously decreasingupward velocity of fluid flow, to create one level where the majority ofpowdered particles do not pass upwards. Those particles which aresmaller than most in the suspension pass upward from the CR and form theFB around the CB.

A regeneration system for a biologic fluid in extracorporeal bloodtreatment comprising:

a housing comprising an interior volume and at least one inlet and atleast one outlet;

a solid filtration module comprising a surface adsorptive agentpositioned within the housing between the inlet and the interior volume;

a bed of sorbent particles positioned within the housing between thefiltration block and the outlet; and

a cone shaped reactor placed below the solid filtration module to createa fluidized bed within it, keeping most of the larger sorbent particleswithin the reactor and allowing the fine particles to flow withperfusing solution to form the above bed of particles.

The regeneration system of claim 1, wherein the filtration module andbed of sorbent particles are arranged within the housing relative to theinlet and outlet such that fluid entering the housing through the inletfluidizes the bed of sorbent particles, and passes through thefiltration block before exiting the housing though the outlet, and thecone shaped reactor is placed below the filtration module, allowingcollection of sorbent particles from the filtration bed which fall offof the filtration module when flow is stopped.

The regeneration system of claim 1, wherein the sorbent particles do notpenetrate the filtration module to exit the housing through the outlet.

The regeneration system of claim 1, wherein the filtration modulecomprises activated carbon.

The regeneration system of claim 1, wherein the filtration modulecomprises a body of compressed activated carbon particles.

The regeneration system of claim 5, wherein the filtration module is aporous activated carbon body selected from the group consisting of acarbon block, a carbon fiber pad, and a nanofiber felt.

The regeneration system of claim 6, wherein the filtration module mayfurther comprise a membrane, screen, filter, or other means, with whichto constrain sorbent particles.

The regeneration system of claim 1, wherein the sorbent particlescomprise calcium phosphate particles, microporous zirconium silicate, animmune-sorbent, or a sorbent capable of binding endotoxin and TNF.

The regeneration system of claim 1, wherein the sorbent particlescomprise particles of one or more ion exchange substances, one or morephysiological electrolyte substances, one or more macromolecular flowinducing agents, or combination thereof.

The regeneration system of claim 1, wherein the sorbent particles have aparticle size of 1-50 microns.

The regeneration system of claim 1, wherein the sorbent particles arepresent in the housing in a volume ratio to create a bed of fine sorbentparticles around the filtration bed of 2-6 mm.

The regeneration system of claim 6, wherein the carbon block comprisessmall pieces of carbon which have high external surface area, and finefeatures which give a short mean pore path length, but which areconstrained or immobilized in a manner to allow perfusion of fluidsaround every particle.

The regeneration system of claim 6, wherein the filtering surface of thecarbon block restrains very small particles of other sorbents besidescharcoal.

The regeneration system of claim 1, wherein the biologic fluid is blood,dialysate, peritoneal fluid, ultrafiltrate, or plasma.

The regeneration system of claim 1, wherein the bed of sorbent particlesis created by passing a fluid containing suspended particles through thefiltering surface of the carbon block or a similar filter, and holdingthe particles in fixed position by continuous flow.

The regeneration system of claim 1, wherein the bed of sorbent particlesallows particles to be used for perfusion and depuration, as in acolumn.

The regeneration system of claim 16, wherein the bed of sorbentparticles provides even flow distribution within the layer of very smallparticles.

The regeneration system of claim 1, wherein the fine sorbent particlesare suspended by an upward flow of dialysate or biological fluid thatexactly equals the sedimentation rate of fine particles.

The regeneration system of claim 15, wherein the suspended particlesmove around within the fluid, mixing evenly with all the passing fluid.

The regeneration system of claim 1, wherein the conical shape of thereactor provides a continuously decreasing upward velocity of fluidflow, to create one level where the majority of sorbent particles do notpass upwards.

The regeneration system of claim 1, wherein sorbent particles which aresmaller than most, pass upward from the conical reactor and form thefiltration bed around the carbon block.

The regeneration system of claim 1, wherein fluid flow continues throughfiltration bed without any significant increase in pressure gradient.

The regeneration system of claim 2, wherein the sorbent particles willre-suspend and apply themselves to the filtration module when flowresumes.

The regeneration system of claim 1, wherein the extracorporeal bloodtreatment is hemoperfusion, continuous veno-venous hemodialysis (CVVHD),continuous veno-venous hemofiltration (CVVH), continuous veno-venoushemodiafiltration (CVVHDF), whole body hyperthermia, plasma treatment,dialysate purification and regeneration, peritoneal dialysatepurification and regeneration, or purification of other circulatingfluids.

The regeneration system of claim 6, wherein the nominal mean pore sizesare in the range of 0.5 □m to 10 □m.

The regeneration system of claim 6, wherein the carbon block may be ofany geometry, including a hollow cylinder or a solid cylinder.

The regeneration system of claim 6, wherein the outer surface of thecarbon block as the filtering surface provides a very large surface areafor filtration, and support of a powdered sorbent bed.

The regeneration system of claim 27, wherein a very large amount of thepowdered sorbent may be applied to the surface of the carbon blockwithout creating a thick layer of the powdered sorbent.

The regeneration system of claim 26, wherein fluid flow is on an inwarddirection normal to the surface of the cylinder.

The regeneration system of claim 27, wherein the large surface area ofthe outside of the carbon block cylinder diminishes the rate of fluidflux or flow rate per cm² of filter surface through the sorbent layer,resulting in increased dwell time.

The regeneration system of claim 30, wherein the decreased flow ratealso decreases the hydraulic pressure drop through each squarecentimeter of the sorbent bed.

The regeneration system of claim 1, wherein the filtration bed has ahigh aspect ratio.

The regeneration system of claim 1, wherein the sorbent particles havelimited affinity for one another to avoid clumping and other undesirableaggregation.

The regeneration system of claim 1, wherein the fluid may comprisesurfactants to prevent clumping or other undesirable aggregation ofsorbent particles.

The regeneration system of claim 1, wherein fluid flow through thesystem is uni-directional.

The regeneration system of claim 8, wherein calcium phosphate willoperate by solubility product to modulate the concentration of calcium,phosphate and bicarbonate in the fluid.

The regeneration system of claim 1, wherein fluid flow is continuous,even if blood flow is ceased, so as to maintain the filtration bed,ensure the continued suspension of the sorbent particles, and preventthe passage of toxins through the carbon block.

The regeneration system of claim 1, wherein the cone shaped reactorpermits an equilibrium between the linear flow velocity of the fluid andthe settling rate of particles, and also allows the fluidized bed tocontinue to operate over a range of fluid flow rates.

The regeneration system of claim 6, wherein the carbon block capturesfine particles of sorbent (particle fines).

The regeneration system of claim 6, wherein further comprising a sterileor non-sterile carbon block.

The regeneration system of claim 6, wherein further comprising areplaceable carbon block.

The regeneration system of claim 40, wherein further comprising thesterile carbon block in a sterile perfusion cartridge.

The regeneration system of claim 40, wherein further comprising asterile carbon block in a sterile fluid circuit.

The regeneration system of claim 1, wherein further comprising areplaceable dialysate bag for the removal of small charged toxins andreplenishment of bicarbonate.

The regeneration system of claim 1, wherein further comprising aseparate infusion pump and infusate reservoir, to provide a continuousaddition of substances to the patient.

The regeneration system of claim 1, wherein the fluid circulation rateis 250 mL/min or 400 mL/min.

The regeneration system of claim 24, wherein when the biologic fluid isperitoneal fluid, the solid filtration module filters white cells andfibrin material from the peritoneal fluid, thus keeping the fluid veryclear on outflow from the peritoneum, and diminishing the tendency forobstruction of inflow and outflow catheters.

The regeneration system of claim 45, further comprising an effluent pumpand reservoir, for continuous exchange of fluid wherein the fluid isdialysate.

The regeneration system of claim 48, wherein the flow of dialysate fromthe infusate reservoir to the effluent reservoir can remove substancesfrom the patient which are not well removed by the carbon block.

The regeneration system of claim 1, wherein further comprising spikeports so that a vacuum is maintained as bags of fluid are connected.

A method of regenerating a biologic fluid during extracorporeal bloodtreatment comprising the steps of:

(i) pumping blood from a patient through a dialyzer;

(ii) withdrawing the biologic fluid from the top of the dialyzer;

(iii) pumping the biologic fluid through a dialyzer circuit, and intofluid regeneration system, wherein the system comprises: (a) a solidblock reactor (SBR), containing a solid carbon block of active carbon;(b) a filtration bed of sorbent particles; and (c) a conical reactorplaced below the solid filtration block to create a fluidized bed ofsorbent particles;

(iv) pumping the biologic fluid from the reactor to a fluid bag;

(v) pumping fluid out of the fluid bag and back to the dialyzer; and

(vi) changing or replacing the carbon block, the fluid bag, or both, asneeded.

The method of claim 51, wherein further comprising the step of passingthe fluid through an inlet in the fluid regeneration system, so that thefluid fluidizes the bed of sorbent particles, and passes through thesolid carbon block before exiting through an outlet of the fluidregeneration system.

The method of claim 51, wherein further comprising the step of creatingthe filtration bed of a very fine powder by passing a fluid containingsuspended sorbent particles through the filtering surface of the solidcarbon block, and then holding the sorbent particles in fixed positionby continued fluid flow.

The method of claim 51, wherein further comprising the step of using thefiltration bed to position or immobilize powdered sorbent particles onthe outside of the carbon block during fluid flow.

The method of claim 54, wherein further comprising the step of using thefiltration bed to allow particles of a few microns in diameter to beused for perfusion and depuration like a column, and provide even flowdistribution within the layer of very small particles.

The method of claim 54, wherein further comprising the step of providinga uni-directional flow of fluid through the solid block reactor, toimmobilize the powdered sorbent particles on the outside of the carbonblock.

The method of claim 54, wherein further comprising the step of settingthe fluid flow to 250 mL/min or 400 mL/min.

The method of claim 51, wherein the conical (cone-shaped) reactor (CR)suspends particles in a fluidized bed in which an upward flow of adialysate or biological fluid exactly equals the sedimentation rate offine particles, causing the particles to move around within thesuspension of fluid, mixing evenly with all the passing fluid.

The method of claim 58, wherein the conical shape of the reactorprovides a continuously decreasing upward velocity of fluid flow, tocreate one level where the majority of powdered particles do not passupwards, and the particles which are smaller than most in thesuspension, pass upward from the conical reactor and form the filtrationbed around the carbon block.

The method of claim 51, wherein the carbon block restrains very smallparticles or fines of other sorbents besides charcoal.

The method of claim 51, wherein further comprising the step of primingthe solid block reactor, which priming excludes harmful air and permitsrapid and easy insertion of the reactor into an existing blood treatmentsystem, comprising: (i) evacuating the reactor to a high vacuum; and(ii) filling the reactor from a standard IV bag.

The method of claim 61, wherein further comprising evacuating thereactor to 25 mm Hg or better.

The method of claim 61, wherein further comprising the step of insertingthe fluid-filled reactor, prior to treatment, without the need forchanges, in a machine used for extracorporeal blood treatment.

The method of claim 51, wherein further comprising the step ofincorporating the fluid regeneration system into the dialysate side ofan extracorporeal blood treatment system.

The method of claim 51, wherein further comprising the step of providinga continuous addition of prescribed substances to the patient by eitherloading the fluid bag with the substances, prior to the start of thetreatment, or adding a separate infusion pump and infusate reservoircontaining the substances.

The method of claim 51, wherein the step of changing or replacing thefluid bag gives a physician the ability to separately control removal oforganic toxins over 100 mw (by rate of fluid flow through the carbonblock) and small, charged inorganic toxins (by rate of exchange of thebags of fluid).

The method of claim 66, wherein the organic toxins removed includecreatinine, indole acetic acid, and para-cresol, and inorganic toxinsremoved include NH₄ ⁺ (from urea), K⁺, Na⁺, H⁺ (causing a loss of bufferin the blood), and H₂PO₄ ⁻.

The method of claim 51, wherein the step of changing or replacing thefluid bag removes small charged toxins from the fluid, and replenishesbicarbonate in the fluid.

The method of claim 51, wherein further comprising the step of choosingor adjusting the concentration of the fluid for fine tuning the removalof small, charged toxins.

The method of claim 51, wherein further comprising the step ofmaintaining fluid flow through the filtration bed when blood flowthrough the dialyzer is stopped.

The method of claim 70, wherein further comprising the step ofcontinuing the flow of fluid through the dialyzer or providing a bypassfor the fluid flow around the dialyzer if such is required.

The method of claim 51, wherein the fluid regeneration system removessubstances such as drugs, small molecular weight toxins, or mediummolecular weight toxins.

The method of claim 72, wherein further comprising the step of varyingthe removal rate of substances, including uremic toxins or beneficialnutrients.

The method of claim 51, wherein further comprising the step of using asterile or non-sterile solid block reactor in the circuit.

The method of claim 74, wherein further comprising the step of usinggamma radiation or any other suitable sterilization method, to sterilizethe solid block reactor.

The method of claim 51, wherein further comprising the step of using asterile solid block reactor in a sterile circuit.

The method of claim 51, further comprising the step wherein when fluidflow is stopped, the sorbent particles fall off of the carbon block andreturn to the fluidized bed.

The method of claim 51, wherein the solid block of active carbon resultsin the rapid sorption kinetics necessary for effective and efficienttoxin removal, coupled with other desirable features such as easyconstraint of the carbon, mechanical simplicity, and low cost.

The method of claim 51, wherein the extracorporeal blood treatment ishemoperfusion, continuous veno-venous hemodialysis (CVVHD), continuousveno-venous hemofiltration (CVVH), continuous veno-venoushemodiafiltration (CVVHDF), whole body hyperthermia, partial bodyhyperthermia, plasma treatment, dialysate purification and regeneration,peritoneal dialysate purification and regeneration, or purification ofother circulating fluids.

The method of claim 61, wherein further comprising the step of spikingand filling the evacuated reactor with one or more bags of primingfluids.

The method of claim 80, wherein further comprising the step of usingstandard sealed IV bag spike ports in the reactor so as to maintain thevacuum as bags of fluids are connected.

The method of claim 80, wherein the priming fluid is an aqueous primingfluid.

The method of claim 51, wherein the biologic fluid is blood, dialysate,peritoneal fluid, filtrate, or plasma.

The method of claim 51, wherein the sorbent particles comprise calciumphosphate particles, microporous zirconium silicate, an immune-sorbent,or a sorbent capable of binding endotoxin and TNF.

A device for whole body hyperthermia treatment comprising a heater, adialyzer, and a dialysate regeneration system of claim 1.

A device for extracorporeal blood treatment for kidney failurecomprising the dialysate regeneration system of claim 1, and a sorbentfor ammonium generated from urea by urease.

The device of claim 86, wherein the sorbent for ammonium is microporouszirconium silicate.

A method of regenerating dialysate comprising flowing dialysate into adialysate regeneration system of claim 1.

A solid carbon block for use in regeneration of biologic fluid inextracorporeal blood treatment.

The use of the solid carbon block of claim 89, wherein theextracorporeal blood treatment is hemoperfusion, continuous veno-venoushemodialysis (CVVHD), continuous veno-venous hemofiltration (CVVH),continuous veno-venous hemodiafiltration (CVVHDF), whole bodyhyperthermia, plasma treatment, dialysate purification and regeneration,peritoneal dialysate purification and regeneration, or purification ofother circulating fluids.

A method of regeneration of a biologic fluid during extracorporeal bloodtreatment comprising using a carbon block in conjunction with at leastone bag of sterile dialysate, said bag containing various salts andbuffers.

A method of sterilizing a carbon block for use in regeneration of abiologic fluid during extracorporeal blood treatment comprising usinggamma irradiation to sterilize the carbon block within a sealed case,wherein said sealed case directs the flow of fluid through the carbonblock.

The use of a carbon block in removal of various toxins from dialysateduring dialysis therapies.

The use of a carbon block in CVVH to regenerate ultrafiltrate from theblood and return the filtrate directly to the patient bloodstream (asreplacement fluid)

The use of a carbon block in CVVHDF (Continuous Veno VenousHemodiafiltration) similarly to CVVHD in order to regenerate thedialysate, the filtrate/replacement fluid, or both.

The use of the solid carbon block of claim 89, wherein the carbon blockis sterile or non-sterile.

The regeneration system of claim 1, for use in the treatment of liverfailure, kidney failure, lupus erythematosus, Wegener's, rheumatoidarthritis, psoriasis, drug overdose, or sepsis.

A disposable solid carbon block reactor for the regeneration of abiologic fluid during extracorporeal blood treatment.

BRIEF DESCRIPTION OF THE DRAWINGS

The above-mentioned and other features of this disclosure, and themanner of attaining them, will become more apparent and the disclosureitself will be better understood by reference to the followingdescription of embodiments of the disclosure taken in conjunction withthe accompanying drawings, wherein:

FIG. 1—Typical Active Carbon Pore Structure Schematic

FIG. 2—Effects of Particle Size on Sorption Kinetics

FIG. 3—Extracorporeal Blood Treatment System Using Suspension of ActiveCarbon

FIG. 4—Theoretical Treatment Efficacy as a Function of Plasma Flow Rate

FIG. 5—Fractal Carbon Spheres

FIG. 6A—Example of a Solid Block Active Carbon Filter

FIG. 6B—Example of a Solid Block Active Carbon Filter

FIG. 7—Solid Carbon Block Flow and Holder/Reactor

FIG. 8—Example Insertion Point of a Solid Block Carbon Reactor to anExisting Disposable Kit for Hemodialysis (B Braun Diapact CRRT Machine)(From Diapact™ manual)

FIG. 9—SBR Disposable

FIG. 10—Auxiliary Priming Disposable

FIG. 11A—Comparison of Biologic DT Circulating Active Carbon Suspensionwith Solid Block Active Carbon Reactor Using Aqueous Dialysate

FIG. 11B—Comparison of Biologic DT Circulating Active Carbon Suspensionwith Solid Block Active Carbon Reactor Using Aqueous Dialysate

FIG. 12A—Performance Comparisons Between Solid Block Carbon and OtherCarbon Forms

FIG. 12B—Performance Comparisons Between Solid Block Carbon and OtherCarbon Forms

FIG. 13—Results of Gamma Irradiation of Carbon Blocks

FIG. 14—Conventional CVVHD

FIG. 15—Modification of Conventional CVVHD Using a Carbon Block

FIG. 16—Combination of Conventional and Carbon Block Methods withInfusate

FIG. 17—Addition of Effluent Pump and Reservoir

FIG. 18A—Calcium Phosphate Powder Without Fluid Flow

FIG. 18B—Calcium Phosphate Powder With Fluid Flow

FIG. 19A—Differences between a standard column and the carbonblock/filtration bed approach

FIG. 19B—Surfactants in the fluid may possibly be included in the fluidto aid in meeting particle size, fluid density and viscosity, otherfluid characteristics, fluid/particle affinity, surface tension, etc.

FIG. 20—Diagram of the heating circuit of the ThermalCore HT Systemwhich includes the DeBakey roller pump and BioTherm heat exchanger, andthe NxStage sorbent-dialysis system.

FIG. 21—CCS Test Apparatus

FIG. 22—Outlet Temperature over Time.

FIG. 23—CBFB Pressure over Time (mmHg)

FIG. 24—CBFB Hydraulic Resistance over Time—mmHg/(mL/min)

FIG. 25—Cone Reactor Hydraulic Resistance over Time (mmHg)

FIG. 26—Cone Reactor at Startup

FIG. 27—Cone Reactor Soon after Startup

FIG. 28—“Mature” Cone Reactor

FIG. 29—Particle Cloud at Highest Point

FIG. 30—Reactor at End of Experiment 1

FIG. 31—Early CBFB Flow Uniformity Test

FIG. 32—CBFB Flow Uniformity Test at End of 4h Run

FIG. 33—CBFB Weight Gain Over Time

FIG. 34—Experiment 2 Total Inlet Pressure over Time

FIG. 35—Experiment 2 Flow

FIG. 36—Cloud In Cylinder Acts As Particle Size Classifier

FIG. 37—CBFB Flow Uniformity

FIG. 38—Experiment 3 Setup

FIG. 39—Experiment 3—Simulated Blood Flow through Biotherm/MCH-1000 overTime

FIG. 40—Experiment 3 CBFB Inlet Pressure over Time

FIG. 41—Experiment 3 “Blood” Pressure over Time

FIG. 42—NxStage Temperature—Trace is Output Temperature of “Blood” toReservoir

FIG. 43—Unitary CCS

FIG. 44 BioLogic—HT Circuit Schematic

FIG. 45—The Combined system

FIG. 46A—Spreadsheet, First worksheet (part 1 of 2): The output forFunnel Reactor Design Calculations

FIG. 46B1—Spreadsheet, First worksheet (part 2 of 2; top): The outputfor Funnel Reactor Design Calculations

FIG. 46B2—Spreadsheet, First worksheet (part 2 of 2; bottom): The outputfor Funnel Reactor Design Calculations

FIG. 47—Spreadsheet, Second Worksheet: The summary of the Funnel ReactorDesign calculations

Corresponding reference characters indicate corresponding partsthroughout the several views. Although the drawings representembodiments of the present disclosure, the drawings are not necessarilyto scale and certain features may be exaggerated in order to betterillustrate and explain the present disclosure.

DETAILED DESCRIPTION OF THE EXEMPLARY EMBODIMENTS

The embodiments disclosed below are not intended to be exhaustive orlimit the disclosure to the precise forms disclosed in the followingdetailed description. Rather, the embodiments are chosen and describedso that others skilled in the art may utilize their teachings.

We envision the combined system to be arranged as in FIG. 45, so thatparticles which are too small to stay within the fluidized bed travelupwards to form the filtration bed around the carbon block. When fluidflow is stopped, the particles falling off of the carbon block willreturn to the fluidized bed.

Section A: Carbon Block for Toxin Removal from Biological Fluids

The use of porous “solid block” active carbon results in the rapidsorption kinetics necessary for effective and efficient toxin removal,coupled with other desirable features such as easy constraint of thecarbon, mechanical simplicity and low cost.

Laboratory data show that porous active carbon block is generally equalto or superior to alternative sorption systems using active carbon.

Additionally, the author has a developed novel method of priming areactor using the above invention which excludes harmful air and permitsrapid and easy insertion of such a reactor into an existing treatmentsystem. The method consists of evacuating the reactor to a high vacuum.When the user fills the reactor from a standard IV bag, the reactor isimmediately ready to use without otherwise difficult to remove entrainedair.

The invention consists of a novel application of an existing product tothe problem at hand. The existing product is the common solid-blockcarbon water filter cartridge. The novel application is to apply thesolid block carbon filter to the field of extracorporeal bloodtreatments, including, but not limited to:

-   -   Hemoperfusion—Direct adsorption of toxins from blood    -   Plasma treatment—adsorption of toxins from patient plasma    -   Dialysate purification and regeneration        -   Single pass purification of dialysate prior to entering the            dialyzer        -   Recirculating dialysate purification—the dialysate fluid is            purified after acquiring toxins across the dialysis membrane            and thence sent back to the dialyzer after the carbon has            adsorbed the toxins.        -   Recirculating dialysate purification where the solid block            carbon purifies the dialysate from tap or other water prior            to beginning of treatment    -   Peritoneal dialysate purification and regeneration        -   Single pass purification of dialysate prior to entering the            dialyzer        -   Recirculating dialysate purification—the dialysate is            purified after acquiring toxins across the peritoneum and            thence sent back to the peritoneum after the carbon has            adsorbed the toxins. In this application, an added value of            the carbon block is that it will filter white cells and            fibrin material from the peritoneal fluid, thus keeping the            fluid very clear on outflow from the peritoneum. This may            diminish the tendency for obstruction of inflow and outflow            catheters.        -   Recirculating dialysate purification where the solid block            carbon purifies the dialysate from tap or other water prior            to beginning of treatment    -   Purification of other circulating fluids such as albumin or        plasma when used in a dialysis or plasmapheresis circuit or        other extracorporeal blood treatment device.

Multiple vendors produce solid block carbon filters for both commercialand consumer use. See FIGS. 6A and 6B for examples, including theKX-5carbon block from Matrixx, Inc.

These solid block filters are solid only in the sense that the activecarbon is a single piece; they are actually porous with nominal meanpore sizes typically in the 0.5 to 10 μm range. They are made by takingpulverized active carbon, mixing it with a binder and extruding orotherwise processing it into a hollow cylinder. Fluid passes through theblock, typically from the outer perimeter of the cylinder, through theactive carbon matrix and thence to the center hole. Although this flowarrangement is generally satisfactory and results in minimal flowresistance, there is no reason why other geometries cannot be used toproduce other combinations of hydraulic characteristics and columnadsorption characteristics. One example of an alternate geometry wouldbe a solid cylinder used in a manner similar to a classic packed columnwhere flow is from top to bottom.

It should be noted that it is the bare carbon block that is of interesthere. Other accessory components of a typical cartridge such as endcaps, sealing rings, preliminary filter wrapping, etc., may or may notbe useful in specific applications and such may be used or omitted asdesired.

A very common use for these filters is for whole-house residentialdrinking water filtration. They remove sediment and other particulates(such as sand from a well) by virtue of their porous structure. Theyalso adsorb undesirable taste and odor causing substances by virtue ofthe active carbon which makes up the porous structure. Some are alsorated to remove certain toxins such as lead or chlorine. Rated flow canbe in the 11 gpm range. Some carbons are also capable of chemisorptionas well as the more usual van der Waals sorption.

Although the sorbent capabilities are of primary interest here, in someapplications, the filtration function may be useful as well.

Such filters typically have the following characteristics: The carbon isa whole piece. Thus, no means is required to constrain the carbon from“leaking out” from the reactor as fluid passes through it. The geometryis complex, resulting in fine features as would be the case withpowdered active carbon. The mean effective pore length is thus small,resulting in rapid sorption kinetics. They are available in differentnominal pore sizes. They are relatively inexpensive, often mass-producedconsumer items. Application is simple. The reactor to contain the solidcarbon block need only admit fluid to the outer perimeter, collect itfrom the center hole and seal the ends of the block. (See FIG. 7). Theyare typically designed for high water flow rates. The hydraulicresistance thus presented even to albumin or plasma at normal dialysisflow rates is modest, typically <200 mmHg.

A Solid Block Reactor (SBR) includes a block of porous, solid blockactive carbon, along with a suitable container which seals the ends andallows proper fluid flow. The SBR will typically also include otherfeatures such as test, evacuation and fill ports, mountingappurtenances, labels, etc.

FIG. 8 shows an example of how the solid block reactor (SBR) containinga solid carbon block of active carbon could be used with an existinghemodialysis system. From the patient on the left, blood is pumpedthrough a dialyzer and then returned to the patient. The dialyzercircuit withdraws dialysate from the top of the dialyzer, pumps itthrough the SBR and thence to a fluid bag. A third pump pumps dialysateout of the fluid bag and returns it to the dialyzer. The difference inflow between the two dialysate pumps creates ultrafiltrate (or aninfusion).

It was found in laboratory testing that the surface tension of fluidstends to permit air to be entrained in the porous active carbon blockfor some considerable amount of time after liquid flow has begun. Suchair has at least two undesirable effects. First, in some machineconfigurations, this air could be returned to the dialyzer or plasmafilter, and thus, for some blood filtration devices, to the patient'sbloodstream. In severe cases, this could cause air emboli. Secondly, airremoves the carbon which it contacts from active participation in toxinsorption.

The novel solution to the air is to evacuate the reactor containing theactive carbon. A vacuum of 25 mm Hg vacuum or better has proven veryeffective. Prior to use, the reactor is spiked and filled with one ormore bags of priming fluid. Standard sealed IV bag spike ports are usedin the reactor so the vacuum is maintained as bags of fluid areconnected. It is important that aqueous priming fluid be used to primethe carbon in all cases since proteinaceous fluids such as albumin tendto foam in the presence of air. An example of such a disposable kitready for vacuum priming is shown in FIG. 9.

An additional benefit is also obtained. Extracorporeal treatmentmachines are “primed” before use by filling the entire fluid pathwaywith fluid prior to connection to the patient. The goals of priming areto exclude air from the circuit, and typically, check out the machineoperation and discharge any impurities in the fluid circuit.

With an evacuated SBR, the SBR is easily filled with fluid from standardIV bags. Thus, the host machine is primed normally, and the nowfluid-filled SBR is then inserted prior to treatment without need forchanges in the machine's existing operating protocol. The SBR thusbecomes simple to install and apply.

It should be noted that vacuum assisted priming is only an option, notnecessarily a requirement; most carbon blocks cease to emit air after 30to 45 minutes after start of priming at 200 mL/min and would take lesstime at higher flow rates.

As shown in FIG. 10, an orifice may be provided to prevent the SBR fromexhausting an IV bag faster than the operator can react to close off anearly empty bag and open a fresh bag. This prevents air in the bag fromentering the SBR.

Laboratory Results

Presented below are comparisons between an active carbon SBR and othermethods of utilizing active carbon as they apply to differenttreatments. These data serve to illustrate the benefits of the SBR anddemonstrate that the use of an SBR does not result in any significantdecrease in therapeutic performance.

The Biologic DT has, as a major labeled use, the treatment of patientswith acetaminophen overdose. This machine uses a circulating suspensionof powdered active carbon on the dialysate side of a flat platedialyzer. The results are compared with a laboratory test using an SBR.No dialyzer was used in this test; the load on the SBR active carbon wasthus the more severe.

In the data in FIG. 11B, the Theoretical Perfect Block Reservoir showsthe concentration of acetaminophen in aqueous dialysate using asimulated 40L patient if the active carbon were a perfect “black hole”for acetaminophen. The Theoretical Kd=0.85 Reservoir is the same data,but assuming the use of a dialyzer in the circuit in order to make thedata comparable to the graph on the left. As may be seen, there ismassive improvement over the older circulating suspension technology.(Note graph scales carefully.)

The SBR was compared with granules and other forms of carbon usinghighly mesoporous carbon block. The dwell time, the time between whenfluid enters the reactor and when it exits, was seven minutes. Dwelltime is simply the volume of the SBR divided by the flow rate. Threedifferent markers, Methylene Blue (MW=320), Albumin (MM≈65 K) and BlueDextran (MM≈2 M) were used with aqueous buffer and a fourth, Bilirubin(MW=585) was used with bovine plasma. In that graph, the “Nanofiber” wassimilar to KX Industries' “Plekx” material.

Finally, the SBR was compared with some cytokines (various MW) which areimplicated as sepsis mediators. Note that the HSDG was optimized forcytokine removal.

The results are shown in FIGS. 12a and 12b . Clearly, the application ofporous solid block carbon to extracorporeal blood treatments isbeneficial and useful.

Another clinical application of the carbon block will likely be in adialysate regenerating circuit that is used to remove toxins whichdevelop during whole body hyperthermia (a potential therapy for cancer).This will be done to provide the same chemical function we had with theBioLogic-HDT system, which used powdered charcoal, a cation exchangerand a precipitated calcium phosphate as a sorbent suspension (describedin Section C). We have collaborated with the KX Company to create carbonblocks containing the same powdered carbon as was included in ourBioLogic-HDT system (derived from coconut shells). We have tested thesecarbon blocks and shown that binding of toxins is essentially the sameas for the powdered carbon in suspension. The carbon block we plan touse will be packaged in a clear plastic housing, evacuated of air, andbe clean but not sterile. It contains about 300 grams carbon and isapproximately 10″ long and 2.5″ in diameter.

Section A-2: Special Applications of Sterile Carbon Block

As described above, regeneration of dialysate during standardhemodialysis can be performed using sorbents which are clean but notsterile. In a treatment of 3-8 hours, bacterial proliferation is not aproblem. However one type of hemodialysis therapy is performed for verylong periods, up to 72 hours, and therefore utilizes sterile dialysate.This type of dialysis is called “Continuous veno-venous hemodialysis” or“CVVHD.” A variation of this therapy is “Continuous veno-venoushemofiltration” or “CVVH.” In this therapy, the removal of toxins is byhemofiltration (convection) across the dialyzer membranes, and sterilefluid is infused to the blood to replace the filtered fluid. Here also,sterile fluid is used for infusion to the blood returning to thepatient. A combination of hemodialysis and hemofiltration techniques isalso used, called CVVHDF. In any of these applications, if the dialysateor hemofiltrate is to be regenerated by carbon block, the carbon blockmust be sterile and provided within in a sterile perfusion cartridge.

Gamma radiation is a practical method for sterilizing many medicaldevices. Carbon is relatively insensitive to gamma radiation; it is usedextensively in nuclear applications as a neutron moderator in nuclearreactors and in high-energy particle accelerator installations toreceive beam dumps. Carbon blocks that are made with binder typicallyuse either polypropylene or polyethylene in various molecular weightformulations. The latter has been shown to withstand gamma radiationdoses up to 1000 kGy. It is thus a reasonable expectation that carbonblocks may be successfully sterilized by gamma radiation, but there doesexist some concern that the pore structure might be modified by thesterilizing gamma dose. To test this concern, four carbon blocks weretested, two of which received a gamma dose measured to have been between35.62 and 37.84 kGy over 1000 minutes.

As may be seen in FIG. 13, there is not a significant difference increatinine adsorption performance; the curves for the two irradiatedblocks are bracketed by the curves of the two non-irradiated blocks.

As described above, granulated carbon has been successfully used indialysis, for example in the REDY, Biologic DT, and Allient machines ina non-sterile circuit. However, in some dialysis therapies, such asCVVHD (Continuous Veno Venous HemoDialysis), treatments are of longduration (up to 72 hours) and require a sterile dialysate circuit. Inmany cases, patient toxin (e.g., bilirubin) or ion (e.g., potassium)loads may be low or it may be deemed desirable to not remove beneficialsubstances from the patient (e.g., glucose). This may particularly bethe case for patients suffering from drug overdose.

By way of an example treatment modality, FIG. 14 shows a simplifiedschematic of CVVHD. The dialyzer provides a bidirectional exchange ofsubstances across the dialyzer for the purpose of equalizingconcentrations of substances in the patient's bloodstream with theconcentrations in the dialysate. This equalization is never perfect, butis a function of relative concentrations, time, and the permeability ofthe dialyzer membrane for a given substance. To move this equalizationprocess forward, there typically must be continual replacement of thedialysate. Thus, the operation of the system is basicallystraightforward; fresh dialysate is simply pumped through the dialyzerinto a waste container. To remove fluid from the patient(ultrafiltrate), the effluent pump pumps more fluid from the dialyzerthan the replacement dialysate pump. The conventional method can requirefairly high volumes of fluid and typically requires careful preparationof the replacement dialysate to assure sterility and purity. In this andsucceeding figures, many required accessories such as blood leak andpressure monitors are not shown.

FIG. 15 shows how a carbon block can be used to purify the dialysate.This purification can take place both with respect to contaminants inthe dialysis fluid as supplied, and also of substances removed from thepatient. Due to the porous nature of the carbon block, air will beemitted from the block for some considerable time, so the arrangementshown or some other method will be necessary to prevent air fromreaching the dialyzer. Such air does not normally enter the patient'sbloodstream across the dialyzer membrane, but it does remove usefulsurface area from the dialyzer.

Those substances which are prescribed to be added to the patient may beloaded into the dialysate bag prior to the start of treatment. During atreatment, the carbon block, the dialysate bag, or both may be changedas needed.

As shown in FIG. 16, instead of, or in addition to, preloading thedialysate bag with prescribed substances, a separate infusion pump andinfusate reservoir may be added in order to provide a continuousaddition of substances to the patient.

FIG. 17 shows another addition; by adding an effluent pump andreservoir, there can be a continuous exchange of dialysate. In thiscase, the flow of dialysate from the infusate reservoir to the effluentreservoir can remove substances from the patient which are not wellremoved by the carbon block. (Note that in the former case, infusatewill be delivered in relatively small amounts, while in this case,infusate will be used to exchange the dialysate in relatively largeamounts.)

In certain other treatment methods, rather than adding infusate to thedialyzer, the infusate or other replacement fluid can be added directlyto the patient's blood before the dialyzer, after the dialyzer or both.This may be done alone or in combination with any of the above describedmethods.

Although CVVHD is used as an example, the concept of using a sterilecarbon block to regenerate all or part of the dialysate is applicable toa wide variety of therapies. Each of these therapies will have its ownspecial plumbing arrangements; such different arrangements fall withinthe scope of this disclosure.

In regeneration of dialysate, carbon removes principally organic toxinsgreater than 100 m.w. This includes many “middle molecules” that havebeen shown to cause illness during kidney failure. However, there aresome smaller and charged toxins of kidney failure that are not removedby carbon, including: urea, phosphate, sodium, potassium and acid. Theacidity of blood is represented by a deficiency in concentration ofvarious bases in the blood, and is corrected by addition of basiccompounds such as bicarbonate. More complicated columns such as the Sorbinclude layers to remove these various small and charged toxins, butthey require some careful management and priming to produce just thedesired changes in body chemistry. With carbon regeneration of dialysatein CVVHD, the removal of larger molecular weight organic toxins can begreatly increased by merely increasing the dialysate flow rate. Instandard CVVHD since the dialysate is sterile, pre-packaged andexpensive, dialysate flow is typically 30-50 ml/min. This slow flowlimits the chemical efficiency (clearance) of the system greatly. Withcarbon-regeneration of dialysate the flow rate can be increased to 400ml/min without any increase in cost except the cost of the column. Theremoval of small charged toxins, and replenishment of bicarbonate can besimply provided by changing the bags of dialysate when required tosupply the needed changes in body chemistry (such as several five literbags per day). The concentration of the dialysate can also be chosen oradjusted for “fine tuning” the removal of the small, charged toxins.Thus, for the first time, CVVHD with charcoal regeneration of dialysategives the physician the capability to control rate of removal of twodifferent types of kidney failure toxins from patients, according totheir needs: larger organic toxins and small charged toxins.

Section B: The Filtration Bed for Immobilizing Small Sorbent Particles.

Introduction The second technology for immobilizing powders which wehave developed is a filtration bed which positions particles on theoutside of the carbon block during fluid flow. For function in ahyperthermia circuit the sorbent used in the filtration bed will becalcium phosphate. The function of the calcium phosphate (CaHPO₄) layeris to absorb one toxin (acid, H+) and to modulate or control levels ofcalcium and phosphate in the dialysate. Working through its solubilityproduct, calcium phosphate will release calcium or phosphate if theirlevels are low in the dialysate. If the levels are high, it will removecalcium and phosphate. The dissolution or creation of calcium phosphateis possible only when there is a very high surface area/weight, meaningvery small particle size (such as a few microns). When employed in theoriginal BioLogic-HDT circuit, the calcium phosphate in the dialysatewas precipitated on the surface of the carbon powder particles and heldin suspension. The suspension moved through the dialyzer, propelled bymembrane motion and vacuum/pressure gradients. In the currentapplication, the calcium phosphate will be a powder that is heldmotionless in a filtration bed around the carbon block. Otherapplications of sorbents also require very small particle size, such asuse of microporous crystals of zirconium silicate, for binding potassiumand ammonium in a dialysate circuit). Note that calcium phosphate isexemplary; other substances may also be used.

At a modest flow rate such as 250 ml/min a finely powdered sorbent, suchas calcium phosphate (CaHPO₄) will form a layer fixed on the outside ofthe carbon block. Fluid flow through the layer proceeds without anysignificant pressure gradient (with 100 grams of calcium phosphate,about 60 mm Hg pressure drop). With perfusion of dialysate around theparticles, calcium phosphate powder can dissociate and deliver solublephosphate whenever the dialysate calcium x phosphate product decreasesbelow the dissociation constant for calcium phosphate, just as it did inthe suspension of the BioLogic-HDT system. The photographs below (FIG.18) show the carbon block and calcium phosphate powder without fluidflow through the carbon block (left) and with fluid flow of 400 ml/min(right). With fluid flow, the calcium phosphate powder is firmly appliedto the outside of the carbon block, but fluid flow continues throughthis filtration bed of particles without any significant increase inpressure gradient (57 mm Hg at 400 ml/min flow rate). When flow isstopped, the calcium phosphate powder falls downward to the bottom ofthe canister (as shown on left), and the powder will re-suspend andapply itself to the outside of the carbon block when flow resumes. Noneof the powdered calcium phosphate penetrates into the block (as shown bysections of the block after use), and no particles permeate the block.The calcium phosphate powder is in intimate contact with all fluidflowing through the filtration bed and apparently, the fluid flow isvery uniform.

Concept of Structure and Function of the Carbon Block/Filtration Bed,and Why Flow and Function is Different from a Standard Sorbent Column

It is helpful to compare the present invention with standard packedcolumns. With a standard sorbent column, large particles or granules areused as sorbent. As discussed above, the finest particles used withinsorbent columns is approximately 50 microns, and this small size allowsuniformly distributed flow without very high pressures only if theparticles are spherical. For applications of carbon in columns theparticle size is usually quite large (such as 1-2 mm) and the individualgranules are easily palpable. To load a standard column, the drygranules or sorbent particles are usually poured into the open column, atop is attached, the column is inverted to begin filling (allowing airto escape) and fluid flow is begun. When the air has been expelled, thecolumn is inverted again. Sometimes the column is filled with fluid andthen the sorbent particles are poured in. Whether filling a wet or drycannister, the force of gravity and chance determine the position ofgranules when perfusion starts. Larger granules are interspersed withsmaller ones. If one area has a greater proportion of large granules ora small channel space, then during fluid flow through the column thischannel will widen and fluid flow here will be more rapid than thatthrough the rest of the portions of the column, as can be demonstratedduring dye injection. The result of this rapid flow is early saturationof the sorbent granules of the channel, and subsequent early“breakthrough” of bound toxins or compounds. Further, the interspersingof large and small granules tends to form a tight pack (much like occurswith use of varying gravel size used in road construction). However, toa large degree, the use of uniformly sized particles, sophisticatedcolumn packing techniques, packing fluids and apparatus can greatlyreduce these problems. Such techniques do, however add significant costto the column. When we have attempted to make a column out of ourcalcium phosphate powder, we have found that when we begin fluid flowthe powder forms a very dense semi-solid “cake” and perfusion pressuresat low flow rates are in the hundreds of mm Hg, for columns that areonly about 1 cm thick.

The method of constructing the outer powdered sorbent layer of thecarbon block/filtration bed device is quite different. The loose andvery fine powder is placed in the bottom of the canister, and the fluidflow is begun. The fluid flow rate exceeds the sedimentation rate of allof the particles and therefore the particles are carried with the fluidagainst the force of gravity. It is likely that during the fluid flowthe finest particles are carried to the surface of the carbon blockfirst, then the larger granules. As the particles form layers around thevarious portions of the carbon block, then hydraulic resistance of eachportion becomes higher and fluid flow automatically re-directs toportions that do not have a powdered bed layer. After the entire carbonblock outer surface is covered, then there are probably still portionswhich have higher flow. However, the higher flow in these channelsbrings with it more sorbent particles and the channels tend to fill andresolve automatically. The powdered bed appears to be less likely topack tightly compared to a standard column. Whereas it required severalhundred mm Hg of pressure to perfuse a standard column created fromcalcium phosphate powder, the carbon block/filtration bed held about 50grams of calcium phosphate powder and when perfused at a rapid rate of250 ml/min had a pressure gradient of about 57 mm Hg.

Another feature of the carbon block/filtration bed that distinguishes itfrom a standard column is the shape of the sorbent layer. Instead ofbeing a cylinder with fluid flow along its axis and a filter at one end,the filtration bed on the carbon block forms as a layer around acylinder with fluid flow on an inward direction normal to the surface ofthe cylinder. The use of the outer surface of the carbon block as thefiltering surface means that there is a very large surface area forfiltration and support of the powdered sorbent bed. This means that avery large amount of powder may be applied to the surface of the carbonblock without creating a thick layer of powder. As an example, one sizeof the Matrixx KX-5 is 2.5 inches in outer diameter and 10 inches long.The circumference is thus about 8 inches and the surface area of theouter portion is about 80 square inches. If this same surface area werecreated as a flat filter at the bottom of a cylindrical column, thediameter would be approximately 10 inches (about 25 cm). If the desiredthickness of the sorbent layer were only 1 cm, this would result in anaspect ratio (width:height) of 25:1 for the column, a configurationwhich would certainly encourage irregular flow. However, with thefiltration bed, it appears that flow is uniform through all parts of thebed (judging from the structure of the bed alone). If a standard columnwere created with a more standard aspect ratio such as 1;1 or less, thento utilize the same amount of powdered sorbent it would require a columnheight many times higher. The longer fluid flow path would greatlyincrease the hydraulic resistance of the column. The large surface areaof the outside of a cylinder has a second advantage, in that itdiminishes the rate of fluid flux through the sorbent layer (flow rateper cm2 of filter surface). The result is increased dwell time whichimproves reaction kinetics. This decreased flow rate also decreases thehydraulic pressure drop through each cm2 of sorbent bed. This benefit isof course another way to describe the benefits of a very high aspectratio for the filtration bed. A simple depiction of differences betweena standard column and the carbon block/filtration bed approach is shownin FIG. 19 a.

Clearly, other variations on this same principle are possible. Forexample, a “column” may be constructed with or without the carbon,having a membrane, filter, screen or other means (designated “screen”hereafter in this paragraph) with which to constrain particles. Multiplegeometries are possible. In all cases, there are three requirements.First, the zero-flow position of the particles must be substantiallyaway from the screen. Gravity would be the normal means of achievingthis, but reverse flow is also a means. Secondly, the particles mustreadily suspend during flow by means of an appropriate combination ofparticle size, fluid density and viscosity, other fluid characteristics,fluid/particle affinity, surface tension, etc. Thirdly, the particlesmust have limited affinity for one another to avoid clumping and otherundesirable aggregation. Surfactants in the fluid may possibly beincluded in the fluid to aid in meeting these requirements. FIG. 19bexemplifies this concept. Also, of course, carbon or other materials orsorbents may be formed into solid porous blocks (in place of the screenof FIG. 19b ) of various shapes by which means fluid volume and spacerequirements may be reduced for a given surface area. A vertical systemis also quite possible; the screen is at the top of a short column oflarge diameter.

Use of Carbon Block/Filtration Bed to Regenerate Dialysate in a DialysisMachine

With the carbon block and filtration bed of calcium phosphate (plus thecone reactor as described below, in some circumstances) we can recreatethe chemical function of the BioLogic-HDT system using a dialysateregenerating system in which dialysate flows uni-directionally throughthe canister. This system is more conventional than was the sorbentsuspension system, is more similar to a standard sorbent column, and iseasily compatible with regeneration of dialysate flowing through astandard hollow fiber dialyzer. The powdered carbon will effectivelyremove almost all organic toxins which penetrate the membranes. Thecalcium phosphate will operate by solubility product to modulate thedialysate concentration of calcium, phosphate and bicarbonate. When anyof these electrolytes become abnormally low, the calcium phosphate willautomatically replenish them. When any of these electrolytes becomeabnormally high, the calcium phosphate will remove them. The DialysisMachine

For treatment of patients in the current protocol we will use the carbonblock/filtration bed canister for removal of toxins from dialysate andprovision of phosphate whenever dialysate phosphate diminishes belownormal. The carbon block/filtration bed will be provided in clean formand incorporated into the dialysate side of a standard NxStage™ System100 dialysis system. The NxStage System 100 is a commercially availablehigh permeability dialysis system that is used in many hospitals forcontinuous dialysis of patients in the ICU. It is also used in treatmentof home hemodialysis patients, usually on a short daily schedule. TheNxStage machine controls ultrafiltration (UF) automatically through useof two dialysate side pumps, two volumetric chambers and anultrafiltration pump. The NxStage system is used in the hospital settingwith pre-mixed 5 liter bags of sterile dialysate (bicarbonate based). Athome, it is often used with a 60 liter bag of lactate based dialysatecreated on site with the PureFlow™ device. Maximum blood flow rate is500 ml/min and maximum dialysate flow rate is 250 ml/min. Inhyperthermic therapy the NxStage dialysis system will be connected inparallel to part of the blood heating circuit, similar to how theBioLogic-HDT was connected in parallel to the blood heating circuit inthe previous BioLogic-HT System. However, with the new system we willcontrol blood flow rate through the dialyzer with the blood side rollerpump of the NxStage device, at a controlled rate of 400 ml/min. We willtherefore be able to remove blood after the roller pump and replace itjust before the heat exchanger, in a co-current mode with all otherblood flow in the HTA portion. In the BioLogic-HDT system blood flow waspassive through the dialyzer, and counter-current to all the other bloodflow, creating significant recirculation of blood through the dialyzer.This recirculation is avoided with the Generation II system.

ThermalCore-HT Circuit Schematic

Blood flow through the heating circuit will be from 1000-2500 ml/min.The following, FIG. 20, is a diagram of the heating circuit of theThermalCore HT System which includes the DeBakey roller pump andBioTherm heat exchanger, and the NxStage sorbent-dialysis system.

3.4 the ThermalCore Ht System Operation

With the NxStage system as the HDT circuit we will use 5 liters ofbicarbonate-based dialysis fluid. This will provide a larger amount ofpotassium and bicarbonate than was present in the two liters of fluid inthe original HDT circuit, and a greater volume of dialysate for removalof potassium if needed (by using a low potassium concentration indialysate). The total capacity for balancing electrolytes should beessentially the same as was present with the original HDT circuitcontaining the electrolyte-balanced polystyrene sulfonate (whichremained mostly loaded with divalent cations calcium and magnesium).Changes in calcium, phosphate and bicarbonate concentration will beoffset through dissolution of precipitated calcium phosphate (powder),as it was in the original HDT system. We will circulate the dialysate at250 ml/min, through the dialyzer, through the charcoal block/filtrationbed canister, and back to the bag. We will not need a heater in theNxStage circuit, as the 5 liters of dialysate should quickly come tonearly the same temperature as the blood within the patient. We expectto set the ultrafiltration rate of the NxStage circuit to zero, but ifit appears the patient has received more fluid than needed, UF could beremoved at up to 1000 ml/hour. This ultrafiltered fluid would accumulatein the 5 liter bag, which is used to prime the entire dialysate side ofthe circuit.

With incorporation of the NxStage System into the ThermalCore HT system,we are using a commercially available and well-proven device to automatethe dialysis circuit, monitor ease of blood flow, detect bubbles,control ultrafiltration, and limit blood side chemical changes.

These features and functions are all similar to those that were includedin the BioLogic-HT System, but we accomplish these functions usingtechnology that appears much more conventional. The many similarities infunction between the original BioLogic-HT System and the current systemare demonstrated by the following Comparison Table:

TABLE # 16 Comparison Table of the Original BioLogic-HDT System and theThermalCore-HDT portions of the Systems: Feature BioLogic-HTThermalCore-HT Dialyzer Cellulosic Flat Plate, Polysulfone hollow fiber,1.8M² 1.6M² Blood Flow Rate 600-800 ml/min with 400 ml/min withoutrecirculation recirculation Dialysate Flow Rate 300 ml/min (net out 250ml/min of dialyzer) unidirectional Creatinine clearance 130 ml/min 150ml/min (in vitro) Ultrafiltration Rate 0-1000 ml/hour Same PowderedActivated 140 grams, Coconut, 300 grams, Coconut, Charcoal in suspensionsupported in carbon block Powdered Calcium 50 grams (80 mM), 50 grams,precipitated by Phosphate USP precipitated in bag manufacturer Potassiumremoval 10 meq 60 meq (from one 5 liter maximum (with bag, a second bagcould be zero potassium used to contribute more) added to bath, patientK of 6) Potassium donation  6 meq Same maximum (starting bath of 6 meq,patient K of 3) Bicarbonate 40 meq Same donation maximum (from 2 literbag) (patient bicarbonate of 10) Phosphate donation 20 mM Same maximum(patient phos of 0.5 mM) Bacteriologic Status Clean, not sterile Same ofdialysate circuit Blood Temperature Outflow of Heater, Same MonitoringInflow Blood Line Patient Temperature Multiple Points Same Monitoring

In terms of function and features, steps of operation, and clinicaleffects we expect the ThermalCore-HDT System to be highly similar tothat used in our prior IDE studies. However, the overall operation willbe much simpler.

There are other potential uses for the carbon block/filtration bedtechnology besides whole body hyperthermia. If the calcium phosphatepowder is replaced by an ammonium sorbent such as a cation exchangerlike powdered microporous fractionated protonated zirconium silicate(ZS, U.S. Pat. Nos. 5,891,417, 6,579,460, 6,099,737, and publishedapplication 2004/0105895), then the carbon block/filtration bedtechnology should be perfect for treatment of liver failure. If theurease enzyme is bound to the ZS or placed in a layer upstream from it,then the system could effectively treat kidney failure (an anionexchanger would also be needed). If an immune-sorbent is used in thefiltration bed and the perfusate is plasma, then various immune diseasesmight be treated such as lupus erythematosus, Wegener's, rheumatoidarthritis and psoriasis. The charcoal also will bind a number ofintermediaries of these immune diseases. Finally, with a sorbent capableof binding endotoxin and TNF (a cytokine) such a system with plasmaperfusion could treat the condition of sepsis.

If there is one down-side of the filtration bed, it is that when fluidflow is stopped, the sorbent particles leave the membranes and quicklyfall to the bottom of the canister. When fluid flow is re-started therewill be some passage of the toxin materials from the bulk fluid throughthe carbon block, until the filtration bed is re-established by theflow. For toxins of low potency to the patient, this is not a problem.For some toxins such as ammonium created by urease, release to thepatient could cause problems. If this is a problem, then there are waysto maintain fluid flow through the filtration bed when blood flowthrough the dialyzer is stopped. The easiest is to merely continuedialysate flow, even if blood flow is ceased through the dialyzer.Dialysate flow could be bypassed around the dialyzer if such isrequired.

We have also found that to form a fluidized bed of small particles theflow rate through the CB must be relatively high, such as 400 ml/min fora CB of 2.5″ diameter and 10″ length. At 250 ml/min the fluidized beddoes not form without agitation of the CB and suspension. Further, theformation of the fluidized bed depends on the particle size of thesuspension and the density of the particles. For particles over 10microns in size of reasonably high density such as over 2 gm/cm3, andrelatively low flow rate, the fluidized bed may not form well at all. Ifthe fluidized bed does form but becomes too thick, then flow through theCB is very irregular.

There are also many other cases in which, in contrast to the discussionsurrounding FIG. 18, powder will not naturally uniformly coat a carbonblock, but will form an uneven layer. By using a cone-created fluidizedbed, very fine particles which are not contained by the cone reactorwill form a uniform layer on the carbon block. As a result, allparticles will either be suspended in the fluidized bed or uniformlycoat the carbon block. This uniform coating naturally occurs becauseonly freely floating particles will reach the carbon block and uniformflow through the block will uniformly distribute them.

For all of these reasons we have decided to combine the CB and FB with aconical reactor containing a fluidized bed. The fluidized bed will workto perfuse fluid through particles that have too high a sedimentationrate to rise and form a fluidized bed around the CB. Those particleswith smaller size will rise and form a layer as FB around the CB, asdescribed below. This layer will be relatively thin and made of smallparticles, and results in a uniform fluid distribution through the CB.

Section C: Cone Reactor with Fluidized Bed for Use in Combination withCB and FB Introduction

The cone shaped reactor is a device to contain a fluidized bed,containing all particles in a suspension with sufficient density andparticle size to remain in the reactor during upward flow of fluid.Initial experiments showed that the sorbent calcium phosphate (CP) formsa “cloud” of relatively dense particles, topped by an area of finerparticles. It was immediately realized that a cone shaped reactor couldpermit an equilibrium between the linear flow velocity of the fluid andthe settling rate of particles and also allow the fluidized bed tocontinue to operate over a range of fluid flow rates.

Initial experiments with an Imhoff cone (similar to a funnel with sides7° off vertical) confirmed this hypothesis. In this experiment, the CPwas placed on top of a frit made of a piece of porous plastic with 35 μmnominal pore size. The cone was provided with a lid with which to returnfluid to the reservoir. It was found that when fines released by thecone returned to the cone, they gradually plugged up the inlet frit andpressure built up unacceptably. This experiment did, however confirm thebasic principle of the cone reactor concept.

At the suggestion of David Carr, a carbon block in an un-modified filterholder was used to catch the fines. This method worked well for bothanhydrous particle sizes and for dihydrous CP. The main findings aresummarized in Table 1.

TABLE 1 Fluid Velocity vs. CP Bed Height Fluid Velocity CP Flow CloudCone at Top of Cloud Type Rate Height Angle (cm/min) Old Anhydrous 25021.5 7 3.8 Old Anhydrous 100 14 7 3.6 New Anhydrous 117 21.5 7 1.78 NewDihydrous 86 21.5 7 1.31

Also, to determine the limits of cone angles, both anhydrous anddihydrous CP were poured into funnels of various angles, includingangles beyond that of the bare funnel by mounting the funnel in aringstand and tilting the ringstand. The CP was allowed to settle andthe funnel surface was examined. Then the funnel was drained at a flowrate determined by gravity and 4.5 mm ID tubing. The funnel surface wasthen examined again for residual powder. It was found that funnel anglesup to 45 degrees off vertical were tolerated, with only a minor dustingof powder on them.

As a result of these experiments, a spreadsheet was created to assist inthe analysis and design of cone reactors for CP. To test the validity ofthe spreadsheet and the functionality of the combination of the conereactor and carbon block with a coating of CP powder, 3 experiments wereperformed. We shall call the combination of carbon block with a bed ofCP on it (CBFB) and a cone reactor a CCS (CBFB plus Cone reactorSystem). The output of the spreadsheet is shown in FIGS. 46 and 47.

Analysis also revealed that while a pure cone reactor would work, thelarge volume of a cone as one goes up in diameter results in fairlyuseless and large extra volume. Hence, a more volume-efficient conereactor uses a cylinder on top of a cone, roughly in shape to anunfritted Buchner funnel. That said however, it was found (see Results)that 1-2 cm of headspace in the cone prior to the cylinder seems toreduce fines emission from the effluent. In fact, an “overloaded” conewill naturally have a level 1-2 cm below the cylinder.

With this information in hand, three experiments were performed.

As may be seen in FIG. 21, following the arrows from the reservoir onthe left, fluid is pumped using a roller pump to the bottom of the conereactor. The effluent from the cone reactor goes to the filter holder,thence to the outside of the carbon in the CBFB, then through the carbonblock to the center hole and out back to the reservoir. The reservoirwas heated to 41+/−1° C., and stirred continuously. Flow and pressuresacross the two reactors were acquired by a proprietary data acquisitionsystem.

The reactor was an ordinary laboratory funnel with sides a 30° anglefrom vertical. A cylinder 15.2 cm inside diameter was placed on top ofthe funnel and sealed with permanently sticky butyl caulk. A top wasprovided for the cylinder with an O-ring and provision to adjust theheight of the top so as to vary the cylinder height and volume.Calculated volumes for the cone reactor were 793 mL for the cone and 905mL for the cylinder giving a total of 2968 mL for a 5 cm headspace. Eachadditional cm is approximately 181 mL.

In each experiment, flow was initially set to approximately 250 mL/min.Conditions were varied as seemed necessary or as thought might yieldinteresting results. The first experiment was designed to test a steadystate condition. The second experiment had more of a goal to “break” thefunctionality of the CCS, and the third experiment was designed to testthe interface with the NxStage machine.

250 mL/min was selected as it was thought that this is the maximumNxStage flow; the maximum is actually 200 mL/min.

TABLE 2 Experiment Conditions Summary Initial Anhydrous InitialExperiment CP Load (g) Flow (mL/min) Headspace (cm) Fluid Remarks 1 50250 9.5 0.9% NaCl 250 mL/min entire run except for short run at 100mL/min and stop-flow test. 2 50 262 5.0 RFP-404 370 mL/min testedwithout ill effect. Also tested at 100 and 160 g without ill effect.Fluid was at room temperature (20 C.) until t = 33 min, then heaterturned on, set to 42 C. 3 33 200 5.0 RFP-404 + NaCl NxStage Machinetesting. Machine had pauses which collapsed CBFB bed.

In FIG. 28, note how there is a line just below the rim of sealant. Thatline is the start of the cylinder. The check valve may just be seenabove the worm drive clamp at the bottom. It is the black ring inside.The check valve was made of half of a rubber stopper, top diameter 13.1mm, bottom diameter 10.9 mm, length 14.2 mm, with a long screw to weightit down and keep it straight. Total mass was 3.54 g. The check valve wasnot intended to stop reverse fluid flow, only keep powder from exitingthe cone reactor during flow stop, a job it did well. In experimentsomitting the check valve, powder consistently entered the influenttubing at zero flow. It should also be possible to use a clamp aroundthe tubing if the screw extends below the cone into the tubing. Thetemporary clamp retains powder during shipping. A similar scheme can beused at the outlet. In production units, other refinements are possiblesuch as using a plastic rod instead of a screw and scoring the plasticrod whose end is attached to the tube. The user bends the tube to breakthe rod at the score to release the check valve for operation.

Observe in FIG. 30 how much lower the suspended CP bed is. Much of theCP has gone to the CBFB. CP not retained by the cone reactor wasdeposited on the carbon in the CBFB as seen in FIGS. 31 and 32.

FIG. 32 shows that no harm had come to the CBFB's flow uniformity, butduring a stop-flow test, some CP was not retained on the carbon and fellto the bottom.

Significant observations included the ability of the CCS to perform wellat 100 mL/min, and partly re-start after a stopped-flow condition.

At the end of experiment 1, the CP in both the CR (Cone Reactor) andCBFB were washed into beakers. The supernatant was sucked off after anovernight settling time, then the remaining substance dried. The CBFBwas found to contain 12.5 g and the CR 32.8 g, including a 5 g loss.Thus, the CBFB ended up with 28% of the CP by weight.

The “natural” cloud height was about 1.6 to 2.2 cm below the start ofthe cylinder. This is not a “hard and fast” rule—due to the stochasticprocesses involved, there is never an actual cessation of particlecarryover to the CBFB.

Experiment 2

As may be seen in FIG. 33, the fluid volume of the CBFB is not more than935 mL. The weight steadily increases; the proportions due to powderaccumulation and air emission are not known.

Significant observations in Experiment 2 included:

-   -   Change in salt solution from NaCl to RFP-404 had no effect    -   Change in startup temperature from 42° C. (Experiment 1) to        20° C. (Experiment 2) had no noticeable effect.    -   CP could be slurry loaded, but larger particles remained in pump        tubing for the duration of the experiment.    -   The ability to successfully slurry load an additional 50 g at        t=60 minutes for a total of 100 g and at another 60 g at t=111        minutes for a total of 160 g, with an increase in cloud size and        particle carryover to the CBFB, but without any drastic effects.    -   The ability to operate at 50% greater than design flow rate with        only additional particle carryover.    -   In the event of an “overload,” where the cloud extends into the        cylinder, the cylinder essentially becomes a “particle        classifier” as seen in FIG. 36.    -   Worst case CBFB powder load did not impair uniform flow through        the carbon.    -   Increasing CP load does significantly increase cloud size.    -   The final CP mass in the CBFB was 28.19 g, and in the CR        131.4 g. Loss was less than 0.5 g. The percent of CP in the CBFB        was 18%, and in the CR 82%.

Experiment 3—NxStage Machine

This experiment was primarily designed to test the interface with theNxStage machine. One objective was to simply test overallfunctionality—would the two systems work together with a significantsafety margin.

In FIG. 38, The box denoted by the red arrow includes a CR followed by aCBFB. The MCH-1000 and Biotherm were simulated by a simple resistance ofabout 80-120 mmHg. Flow through the CCS was 200 mL/min. Flow through thesimulated Biotherm/MCH-1000 was typically about 754 mL/min.

To test the ability of the NxStage machine to tolerate the CCS with agood safety margin, three tests were performed, which, along withperiodic machine starts and stops will explain FIGS. 39, 40 and 41.

In the first test, an adjustable flow restrictor was placed in the CBFBeffluent line. The effects may be seen at t=50 to t=60 in FIG. 40. TheNxStage machine did not give any alarms or error indications. Theapproximate 300 mmHg limit was the operator's comfort limit.

In the second test, note in FIG. 38 that both the venous and arteriallines are essentially at the same pressure. A flow restrictor was placedat the outlet of the blood line (returned to the “patient”). The effectsmay be seen from t=60 to t=68 in FIG. 41. The machine generated alarmsat 125, 156 and 143 mmHg. The reader is cautioned that the machinealgorithms with respect to rise and fall times, time delays and limitsare not known and should be determined from the manufacturer.

In the third test, the main blood flow pump was suddenly turned off oron, as may be seen at t=69 to t=75. In all cases, the pump could besuddenly started without a response from the machine. However, if thepump was suddenly stopped the machine would generate a non-fatal alarm.The pump could be stopped by a ramp-down over a period of veryapproximately 3-5 s without generating an alarm.

The NxStage also never complained about the temperature of the blood.See FIG. 42.

Three times however during the final 115 minutes of the experiment, theNxStage machine stopped dialysate flow. The duration and spacing ofthese pauses is apparently random. During the final pause, the CP bed onthe CBFB collapsed. At no time was uniformity of flow impaired, butunused CP was left at the bottom of the filter holder.

The CP level in the funnel was noticeably lower than in earlierexperiments. Unfortunately, the measurements are lost due to a change inthe funnel configuration that was overlooked.

NxStage Operating Notes

-   -   The NxStage machine has a maximum DFR of 200 mL/min (recently        increased to 400 ml/min).    -   The return from the CCS needs to go to a separate bag port than        the main port to avoid adjacent lines ingesting air. It would        also appear helpful to raise this port slightly to keep air well        away from the main port. This will require a dual-male luer        connector not provided with the disposables kit from NxStage.    -   It is necessary to break the “frangible seal” on the extra bag        port.    -   The line with the green clamp needs to be connected to the bag.

Recommendation

FIG. 43 (not to scale) is a schematic of a significant refinement of anidea suggested by Dr. Steve Ash. The issue with pauses can be eliminatedif the falling CP is returned to the cone reactor. Additionally, thenumber of modifications to the original CBFB system have becomesufficiently extensive as to warrant a fully custom unit. In FIG. 43,the inlet check valve is not shown. The cone plus cylinder version ofthe cone reactor is used. Directly on top of it is a carbon block tocreate a CBFB. The lower, inner hole of the carbon block is plugged.Flow begins at the bottom, proceeds to the carbon area, goes through thecarbon into the inner hole in the carbon and out the top outlet. It maybe found expedient to fill the bottom lip of the carbon filter end capto keep it from trapping falling CP. Alternatively, a block without anend cap may be used and a blank plate substituted.

Detailed design of an actual CCS as shown in FIG. 43 must await one ortwo additional experiments and work authorization.

CONCLUSIONS AND SUMMARY

Definition: CCS a combination of a CBFB+a Cone Reactor System.

Evacuating the CBFB is may be contraindicated for some applicationsunless it is filled off-line. The CBFB may thus be either filledoff-line or shipped filled with liquid. In the latter case, the CBFBneeds to be well shaken before use.

A CCS, or CBFB may possibly need to be placed on the floor or a table toavoid disturbance due to machine vibrations. Excessive vibrations fromsome machines could disturb the filter bed.

Cone reactor hydraulic resistance is negligible, about 10 mmHg at 250mL/min. Fittings will do that. (Note that a 31 inch height difference inwater levels produces about 60 mmHg pressure differential.)

There should not be a distributor in a cone reactor. A check valveconsisting of an elastomeric plug with a long rod extending into theinlet tube acts as a weight and retainer. This simple method keepspowder out of the lines during shutdown. A clamp on a tube can hold therod tight against the funnel inlet to keep powder contained duringshipping. Other methods are possible as well.

Effective dwell time is some fraction, around 0.8 of cone volume, notentire reactor volume, divided by flow.

A cone reactor performs well at any flow which places the cloud top lessthan about 2 cm of top of cone. In this case, the filter bed will berelatively thin.

Higher flows push the cloud into cylinder. The cylinder then acts as aclassifier and retains larger particles while sending smaller ones toCBFB. In this case, the filter bead will be relatively thick.

A good length of time, about 3 h is required to fully evaluate a CCS.This is due to the statistical nature of fluid and particle flow. Thisdoes not imply that the adsorption kinetics of the powder changesignificantly during this startup time.

Particle transfer is a function of fluid mechanical and thermodynamicprobabilities, as well as the particle size distribution. The situationis analogous to water in a pan on the stove. Eventually it willevaporate. Turn on the gas and it will boil. But the process isessentially the same. Thus, particles are continuously, at some rate,transferred from the CR to the CBFB.

Cloud volume, to a large degree, is a function of the amount of CPloaded into the system.

At end of experiment 1, 50 g of CP put 13 g on the CBFB, leaving therest (72%) in the CR. (12.5 g/32.8 g=˜28% in CBFB, 72% in CR—˜5 g lost).In the second experiment, 18% was in the CBFB and 82% in the CR. In thethird experiment 12.5 g was on carbon, and 34.6 g in CR, for 27% and 73%respectively.

Since the CBFB receives the smallest particles from the CR at a slowrate, the buildup on the CBFB is uniform. Flow is uniform through theblock.

Due to the stochastic nature of particle retention and transfer,“overloads” of the CCS, whether from excessive flow rate or excessive CPload, smoothly transfer CP mass to the CBFB at an increasing ratewithout sudden breakdowns of the process. This assumes that nothing isgrossly undersized.

Depending upon schedule, it is possible that further refinements may bemade in the design. E.g., it is not known at what point the CBFB becomesactually overloaded and fails to provide uniform distribution.

CBFB resistance goes up initially, then down with time. This is likelyto be a function of fluid temperature, possibly from changes in fluiddensity or increased Brownian motion. Particle dissolution could also bea factor.

The 9 to 11 μm particle size Anhydrous CP seems to have a fairly widedistribution. Some particles remained in pump tubing during slurry fill.

Under some conditions, slurry fill of powder may be possible with veryfine powders. This may be useful if a powder must be added to an alreadyrunning system.

A cone reactor may be restarted after 25 minutes.

A CBFB with a light coating will start falling off after about 25minutes after a stop-flow event. Data suggests that hold-up time may bea function of trapped air continuing very small flow for a time.

Comparing dwell time to dissolution data indicates reasonablefeasibility.

Crude estimate of CP needed: 250 mL/min*60 min/h*3 h/1000=45 L. 45 L*0.2g/L=9 g. Another source gives 0.316 g/L at 38° C., for 14.2 g. Using 50g given to FDA, corrected for molar ratios gives a dihydrous load of63.5 g, which should be enough.

The combined CCS of FIG. 43 has significant advantages and may be easilymanufactured by any competent machinist in prototype quantities or inlarge quantities by normal plastic injection or blow molding.

Section D: Prior Art Use of a Suspension Powdered Sorbents for DialysateRegeration, the BioLogic Series of Devices

The following is a description of prior art for using powdered sorbentsto regenerate dialysate in an extracorporeal circuit. The prior devicewas the BioLogic-HDT™ system, with a suspension of powdered sorbentswhich passed directly through a plate cellulosic dialyzer.

The BioLogic-HDT™ System

An important advance in whole body hyperthermia came with the use of adialysis system with sorbents to remove various organic toxins and tolimit changes in various electrolytes such as phosphorus and bicarbonateduring treatment. This was accomplished in our prior studies of PISHthrough use of an adaptation of the BioLogic-DT (Liver Dialysis)machine. The DT machine had a suspension containing activated charcoalpowder to remove organic toxins, and a sodium-loaded cation exchangerpowder (polystyrene sulfonate, PSS) to remove small amounts of potassiumand ammonium. In the HDT system we also precipitated 80 mM of calciumphosphate within the sorbent suspension (50 grams). Through dissolution,the calcium phosphate precipitate would increase the phosphate level indialysate if it was lowered by a decreasing phosphate concentration inthe blood. We also changed the loading of the cation exchanger so thatit was in equilibrium with the normal plasma levels of potassium,magnesium, calcium and hydrogen. In this way, the PSS would release asmall amount of these cations into dialysate if concentrations fellbelow normal, and absorb a small amount if the concentrations rose abovenormal. The automatic control of changes in dialysate chemistry wouldthen offset and diminish changes in chemical concentration in the bloodduring whole body hyperthermia treatment (WBHT) therapy (calledperfusion-induced systemic hyperthermia (PISH) if perfusion-induced).

Description of the Biologic-HDT Machine

The following is our description of the Biologic-HDT dialysis circuitfrom our 1996 Food and Drug Administration Investigational DeviceExemption (IDE) (G960257/S) for a clinical trial of WBHT in treatment ofpatients with advanced lung carcinoma (page 6 of the Operator's Manual):

“The dialysate side contains a 2-liter suspension of powdered sorbents(charcoal and cation exchanger) which circulates between the dialyzerand a bag, and controls chemical composition of the dialysate accordingto binding characteristics and loading of the sorbents. Theultrafiltration rate is measured by changes in weight of the sorbentbag; simple algorithms adjust the ratio of blood inflow and outflowcycle times to obtain the minimal ultrafiltration rate, andautomatically reinfuse fluid to the patient to obtain exactly theprescribed weight increase or decrease during treatment. The sorbentcomponents of the BioLogic-HDT machine were as follows:

-   -   1. 200 grams of cation exchanger, pre-loaded with sodium,        calcium, potassium, hydrogen, and magnesium in amounts to        maintain equilibrium with normal blood concentrations,    -   2. 140 grams of powdered activated charcoal with 80 mMoles of        calcium phosphate (50 grams) precipitated on the surface to        dissociate whenever the surrounding solubility product is lower        than the normal blood solubility product,    -   3. Sodium bicarbonate and sodium chloride in physiologic        concentrations,    -   4. Flow-inducing agents,    -   5. And glucose absorbed to the powdered charcoal to dissociate        and maintain normal or slightly high blood glucose.

Additional calcium chloride is infused into the venous return line ofthe HT at a rate necessary to maintain a normal blood calciumconcentration. In-room analysis of plasma phosphate prompts addition ofdisodium phosphate to the sorbent suspension whenever plasma phosphatedecreased below normal levels (which happens only during hightemperature WBHT). From previous studies, a solution of disodiumphosphate and sodium bicarbonate was devised which, when added to thesorbent suspension during high-temperature PISH, should result in normalblood chemistries at the end of the procedure, eventually obviating theneed for performing blood chemical analysis during PISH.”

The BioLogic-HDT system contained a plate dialyzer in which membraneexpansion and compression mixed the sorbent suspension at the membranesurface. In the BioLogic-HDT system blood through the dialyzer waspassive, created by positive pressure on the return limb of the bloodcircuit, and carrying blood back to the inflow limb where pressures werenegative. Blood flow rates were 1500-2000 ml/min through the rollerpump/heating circuit and 600-800 ml/min through the dialyzer. Bloodflowing through the HDT portion returned to the inflow side of theroller pump, so there was some recirculation of treated blood throughthe dialysis system. Sorbent was circulated by alternating pressure in areservoir on the outflow side of the dialyzer. The following diagram ofthe circuit was included in our 1996 IDE Application:

BioLogic-HT™ Circuit Schematic

The BioLogic-HT Circuit is shown in FIG. 44.

Results of Clinical Trial with the BioLogic-HT system

Clinical trials of the BioLogic-HT system demonstrated that during PISHwith this system there were minimal changes in calcium, magnesium,phosphate and serum bicarbonate. Further, the patients remainedphysiologically stable with modest fluid replacement, during the WBHTtreatments.

After initiation of our clinical trials of the BioLogic-HT system intreatment of patients with cancer we received FDA approval to market theBioLogic-DT system for treatment of hepatic failure with coma or drugoverdose. Initial marketing efforts of this treatment were highlysuccessful, but wider market entry was limited by the need for aspecialized machine for this therapy, requiring installation of a newmachine and training at each hospital planning to treat patients withliver failure or drug overdose. Currently the BioLogic-DT system is nolonger available through its manufacturer, and the plate dialyzer is nolonger available. The BioLogic-DT system with some modifications was thedevice used in the BioLogic-HT System.

In terms of other prior art, another method for constraining powderedsorbents to allow perfusion is a “nanofiber” felt. If layers ofnanofiber polymeric materials are bound to powdered sorbents and theneither rolled up or layered, the fine powder particles are heldmotionless during perfusion. There are almost no fines released duringperfusion and flow distribution is good. The downside is that there is avery low packing density. Only about 10% of the volume of the nanofiberfelt layers is due to the sorbent particles. By comparison, the carbonblock and filtration bed are each more than 80% by weight and 50% byvolume of powdered sorbent.

Another technology we developed for powdered sorbent regeneration ofbiologic fluids was to create a bidirectional flow of plasma from bloodthrough membranes, allowing the filtrate to contact powdered sorbents ina suspension transiently and then return to the blood. This applicationwas implemented in the BioLogic-PF for plasma depuration, and also wasshown to work with hemofiltration membranes (membranes which allowpassage of mostly protein-free fluid). In summary, there are fourmethods for restraining fine particles. In summary, there are five waysto restrain powdered sorbent particles in order to perfuse them withfluid for effective depuration and regeneration: Nanofiber felt bed,Solid extruded block, Sorbent suspension passing through a flat-platedialyzer, Bidirectional filtration across hollow fiber membranes into asorbent suspension, and a filtration bed applied by hydraulic flowaround a cylindrical filter. Of these five approaches, we have inventedthe last three.

While this disclosure has been described as having an exemplary design,the present disclosure may be further modified within the spirit andscope of this disclosure. This application is therefore intended tocover any variations, uses, or adaptations of the disclosure using itsgeneral principles. Further, this application is intended to cover suchdepartures from the present disclosure as come within known or customarypractice in the art to which this disclosure pertains.

What is claimed is:
 1. A method of regenerating a biologic fluid duringextracorporeal blood treatment comprising the steps of: (i) pumpingblood from a patient through a dialyzer; (ii) withdrawing the biologicfluid from the top of the dialyzer; (iii) pumping the biologic fluidthrough a dialyzer circuit, and into fluid regeneration system, whereinthe system comprises a solid block reactor (SBR), containing a solidcarbon block of active carbon; (iv) pumping the biologic fluid from thereactor to a fluid bag; (v) pumping fluid out of the fluid bag and backto the dialyzer; and (vi) changing or replacing the carbon block, thefluid bag, or both, as needed.
 2. The method of claim 1 wherein thefluid regeneration system comprises a filtration bed of sorbentparticles; and a conical reactor placed below the solid filtration blockto create a fluidized bed of sorbent particles.
 3. The method of claim2, further comprising the step of passing the fluid through an inlet inthe fluid regeneration system, so that the fluid fluidizes the bed ofsorbent particles, and passes through the solid carbon block beforeexiting through an outlet of the fluid regeneration system.
 4. Themethod of claim 2, further comprising the step of creating thefiltration bed of a very fine powder by passing a fluid containingsuspended sorbent particles through the filtering surface of the solidcarbon block, and then holding the sorbent particles in fixed positionby continued fluid flow.
 5. The method of claim 2, further comprisingthe step of using the filtration bed to position or immobilize powderedsorbent particles on the outside of the carbon block during fluid flow.6. The method of claim 3, further comprising the step of using thefiltration bed to allow particles of a few microns in diameter to beused for perfusion and depuration like a column, and provide even flowdistribution within the layer of very small particles.
 7. The method ofclaim 6, wherein the carbon block restrains very small particles orfines of other sorbents besides charcoal.